A method of producing hexene includes: passing a feed stream comprising c #1# 1 to c24 hydrocarbons through a distillation column, wherein a reflux ratio of the distillation column is greater than or equal to 1.33; distributing a light fraction comprising c4-c6 hydrocarbons to a top portion of the distillation column; distributing a heavy fraction comprising c8-c12 hydrocarbons to a bottom portion of the distillation column; and withdrawing a top product comprising hexene from the distillation column.
|
#1# 1. A method of producing hexene, comprising:
passing a feed stream comprising c1 to c24 hydrocarbons through a distillation column, wherein a reflux ratio of the distillation column is greater than or equal to 1.33;
distributing a light fraction comprising c4-c6 hydrocarbons to a top portion of the distillation column;
distributing a heavy fraction comprising c8-c12 hydrocarbons to a bottom portion of the distillation column; and
withdrawing a top product comprising hexene from the distillation column.
#1# 17. A method of producing hexene, comprising:
passing a feed stream comprising 1-hexene, 1-octene, 1-butene, water, and toluene through a distillation column, wherein a reflux ratio of the distillation column is 1.35 to 1.40;
distributing a light fraction comprising 1-hexene and 1-butene to a top portion of the distillation column;
distributing a heavy fraction comprising 1-octene and toluene to a bottom portion of the distillation column;
withdrawing a top product comprising hexene from the distillation column, wherein the top product comprises less than or equal to 1 parts per million toluene; and
withdrawing a bottom product comprising 1-octene and toluene from the distillation column.
#1# 20. A system for producing hexene, comprising:
a distillation column comprising
a top portion; and
a bottom portion;
wherein the distillation column is configured to:
separate a feed stream into a light fraction and a heavy fraction, wherein a reflux ratio of the distillation column is greater than or equal to 1.33;
distribute the light fraction to the top portion of the distillation column, wherein the light fraction comprises c4-c6 hydrocarbons;
distribute the heavy fraction to the bottom portion of the distillation column, wherein the heavy fraction comprises c8-c12 hydrocarbons; and
release a top product from the top portion of the distillation column, wherein the top product comprises hexene.
#1# 2. The method of
#1# 3. The method of
#1# 4. The method of
#1# 5. The method of
#1# 6. The method of
#1# 7. The method of
#1# 8. The method of
#1# 9. The method of
#1# 10. The method of
#1# 11. The method of
#1# 12. The method of
#1# 13. The method of a
#1# 14. The method of
#1# 15. The method of
#1# 16. The method of
#1# 18. The method of
#1# 19. The method of
|
|||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||
This application is a 371 of International Application No. PCT/M2016/058062, filed Dec. 28, 2016, which claims priority to U.S. Application No. 62/273,021, filed Dec. 30, 2015, both of which are incorporated herein by reference in their entirety.
Hexene remains an important and commercially valuable product in the petrochemical industry. For example, 1-hexene comonomer can be copolymerized with ethylene to produce a flexible form of polyethylene. Another use of 1-hexene is the production of the linear aldehyde heptanal via 1-hexene hydroformylation.
Hexene is often isolated from a mixture of several different hydrocarbons. For example, hexene is often separated from other hydrocarbons through the use of a distillation tower. These conventional hexene isolation methods result in significant impurities in the hexene product. Accordingly, additional processing and purification procedures must take place. These additional processes are often costly and highly inefficient.
Thus, there is a need for an efficient method of isolating hexene from a hydrocarbon mixture that results in a product with minimal impurities and does not require costly purification procedures.
Disclosed, in various embodiments, are processes and systems for producing hexene.
A method of producing hexene, comprises: passing a feed stream comprising C1 to C24 hydrocarbons through a distillation column, wherein a reflux ratio of the distillation column is greater than or equal to 1.33; distributing a light fraction comprising C4-C6 hydrocarbons to a top portion of the distillation column; distributing a heavy fraction comprising C8-C12 hydrocarbons to a bottom portion of the distillation column; and withdrawing a top product comprising hexene from the distillation column.
A method of producing hexene, comprises: passing a feed stream comprising 1-hexene, 1-octene, 1-butene, water, and toluene through a distillation column, wherein a reflux ratio of the distillation column is 1.35 to 1.40; distributing a light fraction comprising 1-hexene and 1-butene to a top portion of the distillation column; distributing a heavy fraction comprising 1-octene and toluene to a bottom portion of the distillation column; withdrawing a top product comprising hexene from the distillation column, wherein the top product comprises less than or equal to 1 parts per million toluene; and withdrawing a bottom product comprising 1-octene and toluene from the distillation column.
A system for producing hexene, comprises: a distillation column comprising a top portion; and a bottom portion; wherein the distillation column is configured to: separate a feed stream into a light fraction and a heavy fraction, wherein a reflux ratio of the distillation column is greater than or equal to 1.33; distribute the light fraction to the top portion of the distillation column, wherein the light fraction comprises C4-C6 hydrocarbons; distribute the heavy fraction to the bottom portion of the distillation column, wherein the heavy fraction comprises C8-C12 hydrocarbons; and release a top product from the top portion of the distillation column, wherein the top product comprises hexene.
These and other features and characteristics are more particularly described below.
The following is a brief description of the drawings wherein like elements are numbered alike and which are presented for the purposes of illustrating the exemplary embodiments disclosed herein and not for the purposes of limiting the same.
The method disclosed herein can provide an efficient method of isolating hexene from a hydrocarbon mixture that results in a product with minimal impurities and without costly purification procedures. For example, the method disclosed herein can produce an overhead 1-hexene product with less than or equal to 1 parts per million toluene impurity. The method disclosed herein also does not use additional fractionation units or adsorber units to purify the hexene product. Accordingly, the method disclosed herein saves significant amounts of capital, energy, and other resources as compared to conventional methods. The method disclosed herein can be efficiently applied to an already exiting distillation column. The method disclosed herein can also leave column parameters such as pressure and temperature unaffected. The method disclosed herein can produce an important and commercially valuable product in the petrochemical industry. For example, 1-hexene comonomer can be copolymerized with ethylene to produce a flexible form of polyethylene. Another use of 1-hexene is the production of the linear aldehyde heptanal via 1-hexene hydroformylation.
1-Hexene is commonly manufactured by two general routes: (i) full-range processes via the oligomerization of ethylene and (ii) on-purpose technology. A minor route to 1-hexene, used commercially on smaller scales, is the dehydration of hexanol. Prior to the 1970s, 1-hexene was also manufactured by the thermal cracking of waxes. Linear internal hexenes were manufactured by chlorination/dehydrochlorination of linear paraffins.
“Ethylene oligomerization” combines ethylene molecules to produce linear alpha-olefins of various chain lengths with an even number of carbon atoms. This approach results in a distribution of alpha-olefins.
Fischer-Tropsch synthesis to make fuels from synthesis gas derived from coal can recover 1-hexene from the aforementioned fuel streams, where the initial 1-hexene concentration cut can be 60% in a narrow distillation, with the remainder being vinylidenes, linear and branched internal olefins, linear and branched paraffins, alcohols, aldehydes, carboxylic acids, and aromatic compounds. The trimerization of ethylene by homogeneous catalysts has been demonstrated.
There are a wide range of applications for linear alpha olefins. The lower carbon numbers, 1-butene, 1-hexene and 1-octene can be used as comonomers in the production of polyethylene. High density polyethylene (HDPE) and linear low density polyethylene (LLDPE) can use approximately 2-4% and 8-10% of comonomers, respectively.
Another use of C4-C8 linear alpha olefins can be for production of linear aldehyde via oxo synthesis (hydroformylation) for later production of short-chain fatty acid, a carboxylic acid, by oxidation of an intermediate aldehyde, or linear alcohols for plasticizer application by hydrogenation of the aldehyde.
An application of 1-decene is in making polyalphaolefin synthetic lubricant basestock (PAO) and to make surfactants in a blend with higher linear alpha olefins.
C10-C14 linear alpha olefins can be used in making surfactants for aqueous detergent formulations. These carbon numbers can be reacted with benzene to make linear alkyl benzene (LAB), which can be further sulfonated to linear alkyl benzene sulfonate (LABS), a popular relatively low cost surfactant for household and industrial detergent applications.
Although some C14 alpha olefin can be sold into aqueous detergent applications, C14 has other applications such as being converted into chloroparaffins. A recent application of C14 is as on-land drilling fluid basestock, replacing diesel or kerosene in that application. Although C14 is more expensive than middle distillates, it has a significant advantage environmentally, being much more biodegradable and in handling the material, being much less irritating to skin and less toxic.
C16-C18 linear olefins find their primary application as the hydrophobes in oil-soluble surfactants and as lubricating fluids themselves. C16-C18 alpha or internal olefins are used as synthetic drilling fluid base for high value, primarily off-shore synthetic drilling fluids. The preferred materials for the synthetic drilling fluid application are linear internal olefins, which are primarily made by isomerizing linear alpha-olefins to an internal position. The higher internal olefins appear to form a more lubricious layer at the metal surface and are recognized as a better lubricant. Another application for C16-C18 olefins is in paper sizing. Linear alpha olefins are, once again, isomerized into linear internal olefins are then reacted with maleic anhydride to make an alkyl succinic anhydride (ASA), a popular paper sizing chemical.
C20-C30 linear alpha olefins production capacity can be 5-10% of the total production of a linear alpha olefin plant. These are used in a number of reactive and non-reactive applications, including as feedstocks to make heavy linear alkyl benzene (LAB) and low molecular weight polymers used to enhance properties of waxes.
The use of 1-hexene can be as a comonomer in production of polyethylene. High-density polyethylene (HDPE) and linear low-density polyethylene (LLDPE) use approximately 2-4% and 8-10% of comonomers, respectively.
Another use of 1-hexene is the production of the linear aldehyde heptanal via hydroformylation (oxo synthesis). Heptanal can be converted to the short-chain fatty acid heptanoic acid or the alcohol heptanol.
The method disclosed herein for hexene production can include passing a feed stream comprising C1 to C24 hydrocarbons through a distillation column. For example, the feed stream can comprise 1-hexene, 1-octene, 1-butene, water, toluene, or a combination comprising at least one of the foregoing. A reflux ratio of the distillation column can be greater than or equal to 1.0, for example, greater than or equal to 1.25, for example, greater than or equal to 1.30, for example, greater than or equal to 1.33. For example, the reflux ratio of the distillation column can be greater than or equal to 1.35. For example, the reflux ratio can be greater than or equal to 1.40. For example, the reflux ratio can be 1.35 to 1.40. The method can include distributing a light fraction comprising C4-C6 hydrocarbons to a top portion of the distillation column. For example, the light fraction can comprise 1-butene, 1-hexene, and water. The method disclosed herein can include distributing a heavy fraction comprising C7-C12 hydrocarbons to a bottom portion of the distillation column. For example, the heavy fraction can comprise toluene, 1-octene, or a combination comprising at least one of the foregoing. The method disclosed herein can include withdrawing a top product comprising hexene from the distillation column. The use of a specific reflux ratio can result in a top 1-hexene product of extremely high purity. For example, the top product can comprise less than or equal to 1 parts per million toluene. A bottom product comprising 1-octene, toluene, or a combination comprising at least one of the foregoing can also be withdrawn from the distillation column.
The method disclosed herein for hexene production can include a feed stream. For example, the feed stream can comprise C1 to C24 hydrocarbons. For example, the feed stream can comprise C1 to C12 hydrocarbons. For example, the feed stream can comprise 1-hexene, 1-octene, 1-butene, water, toluene, ethylene, ethane, propylene, or a combination comprising at least one of the foregoing.
The method disclosed herein can comprise passing as feed stream through a distillation column. The distillation column can comprise a top portion and bottom portion. The distillation column can be a packed bed or trayed distillation column. The distillation column can comprise steel, other metals, ceramics, polymers, or a combination comprising at least one of the foregoing. A reflux ratio of the distillation column can be greater than or equal to 1.33. For example, the reflux ratio of the distillation column can be greater than or equal to 1.35. For example, the reflux ratio can be greater than or equal to 1.40. For example, the reflux ratio can be 1.35 to 1.40. Operating conditions for the distillation column can include a temperature of 80 to 200° C., for example, 85 to 190° C., for example, 88 to 182° C., for example, 90 to 175° C. and a pressure of 3 to 10 barg (0.3 to 1.0 MegaPascals (MPa), for example, 3.5 to 7.5 barg (0.35 to 0.75 MPa), for example, 4 to 4.5 barg (0.4 to 0.45 MPa)).
The method disclosed herein for hexene production can include separating a feed stream into a light fraction and a heavy fraction. For example, the method disclosed herein can include distributing a light fraction to a top portion of a distillation column. For example, the light fraction can comprise C4-C6 hydrocarbons. In the method, a water stream can optionally be included to adjust the flow to result in less C7 hydrocarbons in the light fraction. For example, the water stream can optionally be included to adjust the flow to result in less C7 hydrocarbons in the C6 portion of the light fraction. For example, the light fraction can comprise 1-butene, 1-hexene, water, or a combination comprising at least one of the foregoing. The method disclosed herein can include distributing a heavy fraction to a bottom portion of the distillation column. For example, the heavy fraction can comprise C7-C12 hydrocarbons. For example, the heavy fraction can comprise toluene, 1-octene, or a combination comprising at least one of the foregoing.
The method disclosed herein for hexene production can include withdrawing products from the distillation column. For example, a top product can be withdrawn from a top portion of the distillation column. For example, the top product can comprise a light fraction comprising C4-C6 hydrocarbons. For example, the top product can comprise 1-hexene, 1-butene, water, or a combination comprising at least one of the foregoing. The top product can comprise less than or equal to 100 parts per million toluene by weight. For example, the top product can comprise less than or equal to 1 parts per million toluene by weight. The method disclosed herein can include withdrawing a bottom product from a bottom portion of the distillation column. For example, the bottom product can comprise a heavy fraction comprising C7-C12 hydrocarbons. For example, the bottom product can comprise toluene, 1-octene, or a combination comprising at least one of the foregoing.
The method disclosed herein for hexene production can produce an important and commercially valuable product in the petrochemical industry. For example, 1-hexene comonomer can be copolymerized with ethylene to produce a flexible form of polyethylene. Another use of 1-hexene can be the production of the linear aldehyde heptanal via 1-hexene hydroformylation.
A more complete understanding of the components, processes, and apparatuses disclosed herein can be obtained by reference to the accompanying drawings. These figures (also referred to herein as “FIG.”) are merely schematic representations based on convenience and the ease of demonstrating the present disclosure, and are, therefore, not intended to indicate relative size and dimensions of the devices or components thereof and/or to define or limit the scope of the exemplary embodiments. Although specific terms are used in the following description for the sake of clarity, these terms are intended to refer only to the particular structure of the embodiments selected for illustration in the drawings, and are not intended to define or limit the scope of the disclosure. In the drawings and the following description below, it is to be understood that like numeric designations refer to components of like function.
Referring now to
TABLE 1
Stream number (in reference to FIG. 1)
12
20
22
Temperature (° C.)
58.8
57.6
180
Pressure (barg) (MPa)
4.2 (0.42)
3.99 (0.399)
4.25 (0.425)
Component mass fraction
Ethylene
3.20E−05
0.000128
6.43E−20
Ethane
6.00E−06
2.40E−05
5.19E−20
Propylene
2.00E−06
8.00E−06
5.57E−18
1-Butene
0.135541
0.542248
4.48E−10
1-Hexene
0.114363
4.57E−01
0.000317
Toluene
0.711701
4.56E−05
0.951767
1-Octene
0.03583
4.46E−08
0.047917
Water
0.002525
0.000971
1.36E−31
The following example is merely illustrative of the hexene production method disclosed herein and is not intended to limit the scope hereof. Unless otherwise stated, all examples were based upon simulations.
A method for hexene production in accordance with the present disclosure 10, and as depicted in
TABLE 2
Stream number (in reference to FIG. 1)
12
20
22
Temperature (° C.)
58.8
57.6
180
Pressure (barg) (MPa)
4.2 (0.42)
3.99 (0.399)
4.25 (0.425)
Component mass fraction
Ethylene
3.20E−05
0.000128
6.43E−20
Ethane
6.00E−06
2.40E−05
5.19E−20
Propylene
2.00E−06
8.00E−06
5.57E−18
1-Butene
0.135541
0.542248
4.48E−10
1-Hexene
0.114363
4.57E−01
0.000317
Toluene
0.711701
4.56E−05
0.951767
1-Octene
0.03583
4.46E−08
0.047917
Water
0.002525
0.000971
1.36E−31
The processes and systems disclosed herein include(s) at least the following embodiments:
A method of producing hexene, comprising: passing a feed stream comprising C1 to C24 hydrocarbons through a distillation column, wherein a reflux ratio of the distillation column is greater than or equal to 1.33; distributing a light fraction comprising C4-C6 hydrocarbons to a top portion of the distillation column; distributing a heavy fraction comprising C8-C12 hydrocarbons to a bottom portion of the distillation column; and withdrawing a top product comprising hexene from the distillation column.
The method of Embodiment 1, wherein the feed stream comprises C1 to C12 hydrocarbons.
The method of any of the preceding embodiments, wherein the feed stream comprises ethylene, ethane, propylene, butene, hexene, toluene, octene, water, or a combination comprising at least one of the foregoing.
The method of any of the preceding embodiments, wherein the distillation column is a packed bed distillation column.
The method of any of the preceding embodiments, wherein the reflux ratio of the distillation column is greater than or equal to 1.35.
The method of Embodiment 5, wherein the reflux ratio of the distillation column is greater than or equal to 1.36.
The method of Embodiment 5, wherein the reflux ratio of the distillation column is 1.35 to 1.40.
The method of any of the preceding embodiments, wherein a temperature within the distillation column is 85° C. to 200° C.
The method of any of the preceding embodiments, wherein a pressure within the distillation column is 0.4 MegaPascals to 0.45 MegaPascals.
The method of any of the preceding embodiments, wherein the light fraction comprises butene and the heavy fraction comprises octene.
The method of any of the preceding embodiments, wherein the top product comprises less than or equal to 45 parts per million toluene.
The method of Embodiment 11, wherein the top product comprises less than or equal to 1 parts per million toluene.
The method of any of the preceding embodiments, wherein the top product comprises 1 to 99 weight percent hexene.
The method of any of the preceding embodiments, further comprising withdrawing a bottom product comprising octene and toluene from the distillation column.
The method of any of the preceding embodiments, further comprising polymerizing the top product to produce polyethylene.
The method of any of the preceding embodiments, wherein the method is free of absorber units.
The method of any of the preceding embodiments, wherein energy consumption of the distillation column is reduced by 5% as compared to a distillation column operated by a different method.
A method of producing hexene, comprising: passing a feed stream comprising 1-hexene, 1-octene, 1-butene, water, and toluene through a distillation column, wherein a reflux ratio of the distillation column is 1.35 to 1.40; distributing a light fraction comprising 1-hexene and 1-butene to a top portion of the distillation column; distributing a heavy fraction comprising 1-octene and toluene to a bottom portion of the distillation column; withdrawing a top product comprising hexene from the distillation column, wherein the top product comprises less than or equal to 1 parts per million toluene; and withdrawing a bottom product comprising 1-octene and toluene from the distillation column.
The method of Embodiment 18, further comprising polymerizing the top product to produce polyethylene.
The method of any of Embodiments 18-19, wherein the method is free of absorber units.
A system for producing hexene, comprising: a distillation column comprising a top portion; and a bottom portion; wherein the distillation column is configured to: separate a feed stream into a light fraction and a heavy fraction, wherein a reflux ratio of the distillation column is greater than or equal to 1.33; distribute the light fraction to the top portion of the distillation column, wherein the light fraction comprises C4-C6 hydrocarbons; distribute the heavy fraction to the bottom portion of the distillation column, wherein the heavy fraction comprises C8-C12 hydrocarbons; and release a top product from the top portion of the distillation column, wherein the top product comprises hexene.
In general, the invention may alternately comprise, consist of, or consist essentially of, any appropriate components herein disclosed. The invention may additionally, or alternatively, be formulated so as to be devoid, or substantially free, of any components, materials, ingredients, adjuvants or species used in the prior art compositions or that are otherwise not necessary to the achievement of the function and/or objectives of the present invention. The endpoints of all ranges directed to the same component or property are inclusive and independently combinable (e.g., ranges of “less than or equal to 25 wt %, or 5 wt % to 20 wt %,” is inclusive of the endpoints and all intermediate values of the ranges of “5 wt % to 25 wt %,” etc.). Disclosure of a narrower range or more specific group in addition to a broader range is not a disclaimer of the broader range or larger group. “Combination” is inclusive of blends, mixtures, alloys, reaction products, and the like. Furthermore, the terms “first,” “second,” and the like, herein do not denote any order, quantity, or importance, but rather are used to denote one element from another. The terms “a” and “an” and “the” herein do not denote a limitation of quantity, and are to be construed to cover both the singular and the plural, unless otherwise indicated herein or clearly contradicted by context. “Or” means “and/or.” The suffix “(s)” as used herein is intended to include both the singular and the plural of the term that it modifies, thereby including one or more of that term (e.g., the film(s) includes one or more films). Reference throughout the specification to “one embodiment”, “another embodiment”, “an embodiment”, and so forth, means that a particular element (e.g., feature, structure, and/or characteristic) described in connection with the embodiment is included in at least one embodiment described herein, and may or may not be present in other embodiments. In addition, it is to be understood that the described elements may be combined in any suitable manner in the various embodiments.
The modifier “about” used in connection with a quantity is inclusive of the stated value and has the meaning dictated by the context (e.g., includes the degree of error associated with measurement of the particular quantity). The notation “±10%” means that the indicated measurement can be from an amount that is minus 10% to an amount that is plus 10% of the stated value. The terms “front”, “back”, “bottom”, and/or “top” are used herein, unless otherwise noted, merely for convenience of description, and are not limited to any one position or spatial orientation. “Optional” or “optionally” means that the subsequently described event or circumstance can or cannot occur, and that the description includes instances where the event occurs and instances where it does not. Unless defined otherwise, technical and scientific terms used herein have the same meaning as is commonly understood by one of skill in the art to which this invention belongs. A “combination” is inclusive of blends, mixtures, alloys, reaction products, and the like.
Unless otherwise indicated, each of the foregoing groups can be unsubstituted or substituted, provided that the substitution does not significantly adversely affect synthesis, stability, or use of the compound. The term “substituted” as used herein means that at least one hydrogen on the designated atom or group is replaced with another group, provided that the designated atom's normal valence is not exceeded. When the substituent is oxo (i.e., ═O), then two hydrogens on the atom are replaced. Combinations of substituents and/or variables are permissible provided that the substitutions do not significantly adversely affect synthesis or use of the compound. Exemplary groups that can be present on a “substituted” position include, but are not limited to, cyano; hydroxyl; nitro; azido; alkanoyl (such as a C2-6 alkanoyl group such as acyl); carboxamido; C1-6 or C1-3 alkyl, cycloalkyl, alkenyl, and alkynyl (including groups having at least one unsaturated linkages and from 2 to 8, or 2 to 6 carbon atoms); C1-6 or C1-3 alkoxys; C6-10 aryloxy such as phenoxy; C1-6 alkylthio; C1-6 or C1-3 alkylsulfinyl; C1-6 or C1-3 alkylsulfonyl; aminodi(C1-6 or C1-3)alkyl; C6-12 aryl having at least one aromatic rings (e.g., phenyl, biphenyl, naphthyl, or the like, each ring either substituted or unsubstituted aromatic); C7-19 arylalkyl having 1 to 3 separate or fused rings and from 6 to 18 ring carbon atoms; or arylalkoxy having 1 to 3 separate or fused rings and from 6 to 18 ring carbon atoms, with benzyloxy being an exemplary arylalkoxy.
All cited patents, patent applications, and other references are incorporated herein by reference in their entirety. However, if a term in the present application contradicts or conflicts with a term in the incorporated reference, the term from the present application takes precedence over the conflicting term from the incorporated reference
While particular embodiments have been described, alternatives, modifications, variations, improvements, and substantial equivalents that are or may be presently unforeseen may arise to applicants or others skilled in the art. Accordingly, the appended claims as filed and as they may be amended are intended to embrace all such alternatives, modifications variations, improvements, and substantial equivalents.
Azam, Shahid, Al-Dughaither, Abdullah Saad, Al-Hamdan, Abdulmajeed Mohammed, Al-Dossari, Adel Saeed
| Patent | Priority | Assignee | Title |
| Patent | Priority | Assignee | Title |
| 2700061, | |||
| 3356590, | |||
| 3428528, | |||
| 5332426, | Jul 29 1992 | Minnesota Mining and Manufacturing Company | Agglomerated activated carbon air filter |
| 5853551, | Jul 24 1995 | Institut Francais du Petrole | Process for the separation of alpha-olefins by distillation of an effluent comprising ethylene and 1-butene |
| 20070185362, | |||
| 20140012059, | |||
| 20150291486, | |||
| 20150299069, | |||
| 20190002373, | |||
| 20190010100, | |||
| EP590883, |
| Executed on | Assignor | Assignee | Conveyance | Frame | Reel | Doc |
| Dec 31 2015 | AL-DUGHAITHER, ABDULLAH SAAD | SABIC GLOBAL TECHNOLOGIES B V | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 046191 | /0619 | |
| Dec 31 2015 | AL-DOSSARI, ADEL SAEED | SABIC GLOBAL TECHNOLOGIES B V | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 046191 | /0619 | |
| Dec 31 2015 | AL-HAMDAN, ABDULMAJEED MOHAMMED | SABIC GLOBAL TECHNOLOGIES B V | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 046191 | /0619 | |
| Jan 06 2016 | AZAM, SHAHID | SABIC GLOBAL TECHNOLOGIES B V | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 046191 | /0619 | |
| Dec 28 2016 | SABIC Global Technologies B.V. | (assignment on the face of the patent) | / |
| Date | Maintenance Fee Events |
| Jun 25 2018 | BIG: Entity status set to Undiscounted (note the period is included in the code). |
| Sep 20 2023 | M1551: Payment of Maintenance Fee, 4th Year, Large Entity. |
| Date | Maintenance Schedule |
| Apr 07 2023 | 4 years fee payment window open |
| Oct 07 2023 | 6 months grace period start (w surcharge) |
| Apr 07 2024 | patent expiry (for year 4) |
| Apr 07 2026 | 2 years to revive unintentionally abandoned end. (for year 4) |
| Apr 07 2027 | 8 years fee payment window open |
| Oct 07 2027 | 6 months grace period start (w surcharge) |
| Apr 07 2028 | patent expiry (for year 8) |
| Apr 07 2030 | 2 years to revive unintentionally abandoned end. (for year 8) |
| Apr 07 2031 | 12 years fee payment window open |
| Oct 07 2031 | 6 months grace period start (w surcharge) |
| Apr 07 2032 | patent expiry (for year 12) |
| Apr 07 2034 | 2 years to revive unintentionally abandoned end. (for year 12) |